Process for the preparation of high performance polypropylene

ABSTRACT

The invention discloses a process for preparing high-performance propylene polymers, the process utilizing a high activity, highly stereoselective Ziegler-Natta catalyst and two or more stages of polymerization carried out under different hydrogen concentrations to prepare propylene polymers having broad molecular weight distribution, wherein non-unifomess of isotacticity of molecular chains of the final propylene polymers is improved by adjusting or controlling stereoselectivity of catalytic active sites under different hydrogen concentrations, namely, making the low molecular weight fraction of the polymers having a higher isotacticity and making the high molecular weight fraction of the polymers having a lower isotacticity, thereby overcoming the drawbacks of the propylene polymers having broad molecular weight distribution known in the art. The resulting final polymers have excellent combined properties, in particular, remarkably improved mechanical properties.

CROSS REFERENCE OF RELATED APPLICATION

The present application claims the priority of the Chinese PatentApplication No. 200610076310.7, filed on Apr. 20, 2006, which isincorporated herein by reference in its entirety and for all purposes.

FIELD OF THE INVENTION

The present invention relates to a process for preparinghigh-performance polypropylenes, and more specifically, to a process forpreparing polypropylenes having excellent performance and broadmolecular weight distributions, of which high molecular weight fractionhas a lower isotacticity and low molecular weight fraction has a higherisotacticity.

BACKGROUND OF THE INVENTION

In general, polypropylene resins having broad molecular weightdistributions (of which polydispersity indexes as measured by arheological method are typically larger than 4.0) exhibit betterperformance, because high molecular weight fraction of the resinsimparts better mechanical strength, creep resistance, etc. to theresins, while low molecular weight fraction of the resins impartsexcellent processability to the resins. Therefore, in some applicationsof high-performance polypropylene resins, such as hot-water pipes, BOPPfilms, etc., propylene polymers having broad molecular weightdistributions are more competitive in comparison with propylene polymershaving narrow molecular weight distributions.

In general, polypropylenes produced by using known high-activityZiegler-Natta catalysts have narrower molecular weight distributions,with their polydispersity indexes (PI values) as measured by arheological method being typically less than 4. Thus, multi-stagepolymerization processes are mostly utilized to broaden the molecularweight distribution of polymers in the art, wherein the individualpolymerization stages produce polymers having different molecular weightso that final polymers have broad molecular weight distribution (MWD).In each polymerization stage, the molecular weight of the polymers canbe controlled by using a molecular weight control agent, such ashydrogen gas, or by altering polymerization temperature.

Such typical multi-stage polymerization processes comprise generally twoor more stages of polymerization, wherein a first stage ofpolymerization is homopolymerization of propylene or copolymerization ofpropylene and an α-olefin carried out in the presence of ahigh-activity, highly-stereoselective Ziegler-Natta catalyst and a lessamount of hydrogen, to provide a propylene homopolymer or copolymerhaving larger molecular weight, and a second stage of polymerization ishomopolymerization of propylene or copolymerization of propylene and anα-olefin carried out, in the same reaction zone or in a differentreaction zone, in the presence of the resulting polymer from the firststage of polymerization and a larger amount of hydrogen, to provide apropylene homopolymer or copolymer having less molecular weight.

It is generally accepted in the art that existing Ziegler-Nattacatalysts are multi-site catalysts, in which those active sites havinggood hydrogen response have poor stereoselectivity, while those activesites having bad hydrogen response have good stereoselectivity. Becauseof this inherent characteristic of the Ziegler-Natta catalysts,isotacticities of fractions having different molecular weight ofpropylene polymers prepared through one-stage polymerization processesor traditional multi-stage polymerization processes (in which no meansis used to adjust isotacticities of polymers produced in differentpolymerization stages) will be contrary to the requirements ofhigh-performance materials, that is, low molecular weight fractions ofthe polymers have low isotacticities, while high molecular weightfractions of the polymers have high isotacticities. Such polymers mayhave many defects in the practical applications. For example, thefractions having low molecular weight and low isotacticities tend tomigrate out from the interior of the materials during processing andduring long-term use of articles, and thus adversely affect theperformance and use of the articles. And the fractions having highmolecular weight and high isotacticities tend to form thick lamellarcrystal in the materials, and this is disadvantageous for someapplications of propylene polymers. For example, when such resins areused to high-speed produce BOPP films, film breaking phenomenon occurslikely.

Thus, the current Ziegler-Natta catalyst-based processes for preparingpropylene polymers having broad molecular weight distributions willcause the formation of a large amount of low molecular weight, lowisotacticity fraction and a large amount of high molecular weight, highisotacticity fraction while broadening molecular weight distribution ofthe polypropylenes, so that it is impossible to obtainperformance-optimized propylene polymers.

SUMMARY OF THE INVENTION

The inventors have now found a process for preparing high-performancepropylene polymers, the process utilizing a high activity, highlystereoselective Ziegler-Natta catalyst and two or more stages ofpolymerization carried out under different hydrogen concentrations toprepare propylene polymers having broad molecular weight distribution,wherein non-uniformness of isotacticity of molecular chains of the finalpropylene polymers is improved by adjusting or controllingstereoselectivity of catalytic active sites under different hydrogenconcentrations, namely, making the low molecular weight fraction of thepolymers having a higher isotacticity and making the high molecularweight fraction of the polymers having a lower isotacticity, therebyovercoming the drawbacks of the propylene polymers having broadmolecular weight distribution known in the art. The resulting finalpolymers have excellent combined properties, in particular, remarkablyimproved mechanical properties.

Thus, an object of the invention is to provide a process for preparing apolypropylene having broad molecular weight distribution, the processcomprising at least the following two stages of polymerization: a firststage of polymerization, which is homopolymerization of propylene orcopolymerization of propylene and an α-olefin carried out in thepresence of a Ziegler-Natta catalyst and a less amount of a molecularweight control agent, for example, hydrogen gas, to provide a highmolecular weight fraction of the polypropylene, and a second stage ofpolymerization, which is homopolymerization of propylene orcopolymerization of propylene and an α-olefin carried out in thepresence of the resulting polymer from the first stage of polymerizationand a larger amount of the molecular weight control agent, to provide alow molecular weight fraction of the polypropylene, wherein the firststage of polymerization employs optionally an external electron donorcompound, and the second stage of polymerization employs an externalelectron donor compound, and wherein the amount and/or kind of theexternal electron donor compound used in the second stage ofpolymerization are/is selected so as to give a final polymer having anisotacticity higher than that of the polymer produced in the first stageof polymerization.

In an embodiment of the process according to the invention, a ratio ofthe output of the first stage of polymerization to the output of thesecond stage of polymerization is in a range of from about 30:70 toabout 70:30, and preferably from about 35:65 to about 55:45.

In an embodiment of the process according to the invention, a ratio ofthe MFR value of the final propylene polymer to that of the propylenepolymer prepared in the first stage of polymerization is in a range offrom about 5 to about 15.

In an embodiment of the process according to the invention, a ratio ofthe isotacticity of the final propylene polymer to that of the propylenepolymer prepared in the first stage of polymerization is larger than 1but less than or equal to 1.2, preferably larger than 1 but less than orequal to 1.1, more preferably larger than 1 but less than or equal to1.05, and especially preferably larger than 1 but less than or equal to1.02.

In an embodiment of the process according to the invention, theZiegler-Natta catalyst used in the first stage of polymerization is areaction product of: a solid catalyst component comprising magnesium,titanium, a halogen and an internal electron donor as essentialcomponents, an organic aluminum compound, and an organic siliconcompound, with a weight ratio of the organic aluminum compound to theorganic silicon compound (sometimes simply referred to as Al/Ti weightratio hereinafter) being in a range of from 10 to 300; and an additionalamount of the organic silicon compound is added in the second stage ofpolymerization so as to give a Al/Ti weight ratio of less than the Al/Siweight ratio in the first stage of polymerization. According to apreferred aspect of this embodiment, the Al/Si weight ratio in the firststage of polymerization is about 2 to about 20 times larger than that inthe second stage of polymerization.

In a preferred embodiment, the process according to the inventioncomprises the first and second stages of polymerization, and the firstand second stages of polymerization are carried out in a first loopreactor and a second loop reactor in series, respectively. According toa preferred aspect of this embodiment, a ratio of the output of thefirst stage of polymerization to the output of the second stage ofpolymerization is approximately in a range of from 35:65 to 55:45,polymerization temperatures in the two loop reactors are controlled at60 to 80° C., and the polymerization is conducted in a liquid phase bulkprocess.

Another object of the invention is to provide polypropylenes havingbroad molecular weight distribution obtainable by the process accordingto the invention. The polypropylenes having broad molecular weightdistribution according to the invention have a polydispersity index offrom 3 to 10, and the isotacticity of the low molecular weight fractionthereof is higher than the isotacticity of the high molecular weightfraction thereof.

Still another object of the invention is to provide biaxial orientedfilms, tubings, flat fibers, or injection mould articles prepared fromthe polypropylenes of the invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The process of the invention will be described in detail below withreference to a continuous process comprising two stages ofpolymerization by way of example. However, it is understood that theprinciples of the invention are applicable alike to a batch process or aprocess comprising more than two stages of polymerization.

Any of high activity, highly stereoselective Ziegler-Natta catalysts forpropylene polymerization known in the art can be used in the process ofthe invention. As used herein, the term “highly stereoselectiveZiegler-Natta catalyst” refers to a catalyst capable of catalyzingpolymerization of propylene to produce a propylene homopolymer having anisotactic index of more than 93%, preferably more than 94%, and morepreferably more than 95%. Such catalysts comprise generally reactionproducts of: (1) an active solid catalyst component (also known asprocatalyst or main catalyst), for example, an activetitanium-containing solid catalyst component, preferably a solidcatalyst component comprising magnesium, titanium, a halogen and aninternal electron donor as essential components; (2) an organic aluminumcompound as a cocatalyst; and (3) optionally, an external electron donorcompound. These catalysts can be used directly or after having beensubjected to a prepolymerization.

Solid Ziegler-Natta catalyst components (procatalysts) as well ascatalysts useful in the process according to the invention have beendisclosed in, for example, Chinese patent application CN85100997A,CN1258680A, CN1258683A, CN1258684A, CN1091748A, CN1330086A, CN1298887A,CN1298888A, and CN1436796A. It is particularly advantageous to employthe solid catalyst components as well as catalysts as disclosed inChinese patent application CN1330086A, CN85100997 and CN1258683A.

As the cocatalyst component of the catalysts, the organic aluminumcompounds are preferably alkyl aluminum compounds, and more preferablytrialkyl aluminum compounds. Examples include, but are not limited to,trimethyl aluminum, triethyl aluminum, tri-iso-butyl aluminum,tri-isopropyl aluminum, tri-n-butyl aluminum, tri-n-hexyl aluminum, andtri-n-octyl aluminum. In the process according to the invention, theorganic aluminum compounds as the cocatalyst component are used inconventional amounts. For example, the organic aluminum compound(s) isused in such an amount that a ratio of the active titanium-containingsolid catalyst component to the organic aluminum compound(s) as thecocatalyst component is in a range of from 1:25 to 1:100, in terms ofmolar ratio of Ti to Al.

In general, in the process according to the invention, the active solidcatalyst component and the organic aluminum compound are added into onlythe first stage of polymerization, and it is not necessary to addadditionally the active solid catalyst component and the organicaluminum compound into the second stage of polymerization. However,adding the active solid catalyst component and the organic aluminumcompound into both the two stages of polymerization is within the scopeof the invention.

The external electron donor component of the Ziegler-Natta catalysts maybe selected from the group consisting of mono- and multi-functionalcarboxylic acids, carboxylic anhydrides, esters of carboxylic acids,ketones, ethers, alcohols, lactones, organic phosphorus compounds, andorganic silicon compounds, with organic silicon compounds beingpreferred. The main function of the external electron donor component isto enhance stereoselectivity of active sites of the catalysts.

Preferred organic silicon compounds useful as the external electrondonor component have a formula R_(n)Si(OR′)_(4-n′) in which 0<n≦3, R(s)is/are independently alkyl, alkenyl, cycloalkyl, aryl, or haloalkyl,having 1 to 18 carbon atoms, or a halogen or hydrogen, and R′(s) is/areindependently alkyl, alkenyl, cycloalkyl, aryl, or haloalkyl, having 1to 18 carbon atoms. Examples include, but are not limited to, trimethylmethoxy silane, trimethyl ethoxy silane, trimethyl phenoxy silane,dimethyl dimethoxy silane, dimethyl diethoxy silane, methyl tert-butyldimethoxy silane, isopropyl methyl dimethoxy silane, diphenoxy dimethoxysilane, diphenyl diethoxy silane, phenyl trimethoxy silane, phenyltriethoxy silane, vinyl trimethoxy silane, cyclohexyl methyl dimethoxysilane, dicyclopentyl dimethoxy silane, di-isopropyl dimethoxy silane,di-isobutyl dimethoxy silane, 2-ethylpiperidino tert-butyl dimethoxysilane, (1,1,1-trifluoro-2-propyl) 2-ethylpiperidino dimethoxy silane,(1,1,1-trifluoro-2-propyl) methyl dimethoxy silane, and the like.

In the process for preparing polypropylenes having broad molecularweight distribution according to the invention, it is required that theactive sites of the catalysts have a higher stereoselectivity under highconcentration of a molecular weight control agent, for example, hydrogengas than that under low concentration of the molecular weight controlagent. Thus, feasible manners of using the external electron donorcompounds include, for example, (1) no external electron donor compoundis used in the first stage of polymerization, while an external electrondonor compound is used in the second stage of polymerization; (2) a lessamount of an external electron donor compound is used in the first stageof polymerization, while a larger amount of the external electron donorcompound is used in the second stage of polymerization; and (3) anexternal electron donor compound providing a polymer having a lowerisotacticity is used in the first stage of polymerization, while anexternal electron donor compound providing a polymer having a higherisotacticity is added in the second stage of polymerization. With usingthe external electron donor compounds in such manners, the low molecularweight fraction of the produced polypropylenes will have higherisotactic index (isotacticity) while the high molecular weight fractionof the produced polypropylenes will have lower isotactic index(isotacticity).

In a preferred embodiment, the same organic silicon compound is used asthe external electron donor component in the first and secondpolymerization stages of the process according to the invention, but theconcentration of the organic silicon compound in the secondpolymerization stage is larger than that in the first polymerizationstage. In a more preferred embodiment, a weight ratio of the organicaluminum compound to the organic silicon compound in the first stage ofpolymerization is controlled as being in a range of from 10 to 300, andpreferably from 30 to 150, and the weight ratio of the organic aluminumcompound to the organic silicon compound in the second stage ofpolymerization is made less than that in the first stage ofpolymerization by adding an additional amount of the organic siliconcompound. Preferably, the Al/Si weight ratio in the first stage ofpolymerization is 2 to 20 times larger than that in the second stage ofpolymerization.

It is noted that, in techniques as disclosed in literatures forpreparing propylene polymers having broad molecular weight distributionthrough multi-stage polymerization, no means is employed to adjuststereoselectivities of the active sites of the catalysts in differentpolymerization stages so that the isotacticity of the high molecularweight fraction of the resulting polymers is higher than that of the lowmolecular weight fraction of the polymers. In contrary, in the processaccording to the invention, the isotacticity of the low molecular weightfraction of the propylene polymers is made higher than the isotacticityof the high molecular weight fraction of the propylene polymers producedin the first polymerization stage by enhancing stereoselectivities ofthe active sites of the catalysts in the second polymerization stage forproducing the low molecular weight fraction of the polymers. Theisotacticity of polypropylenes may be characterized by an isotacticindex as measured according to GB 2142-89, or by two parameters asmeasured by ¹³C-NMR spectroscopy, i.e., pentad ([mmmm]) content by moleand average length of isotactic sequences. The larger the valuesmeasured by these methods, the higher the isotacticity of thepolypropylene. Such data can demonstrate the effects of the invention.

In the process for preparing polypropylenes having broad molecularweight distribution according to the invention, the first and secondstages of polymerization are performed under different concentrations ofa molecular weight control agent, for example, hydrogen gas, in order tomake the final propylene polymers having broadened molecular weightdistribution. In general, melt flow rate (MFR) of a final polymer may becontrolled depending on the intended use of the polymer, and the MFR ofthe propylene polymer produced in the first polymerization stage can beso controlled that a ratio of the MFR of the final propylene polymer tothe MFR of the propylene polymer produced in the first polymerizationstage is in a range of from about 5 to about 15. For example, when thefinal polymer will be used as a tubing material, the MFR of thepropylene polymer produced in the first polymerization stage can becontrolled as being in a range of from 0.01 to 0.03 g/10 min., and theMFR of the final propylene polymer can be controlled as being in a rangeof from 0.1 to 0.3 g/10 min.; and when the final polymer will be used asa film material, the MFR of the propylene polymer produced in the firstpolymerization stage can be controlled as being in a range of from 0.2to 0.4 g/10 min., and the MFR of the final propylene polymer can becontrolled as being in a range of from 2 to 4 g/10 min. The MFR valuesare measured according to ISO1133, at 230° C., under 2.16 kg loading.

In the process according to the invention, a ratio of the output of thefirst stage of polymerization to the output of the second stage ofpolymerization may be in a range of from 30:70 to 70:30, preferably from35:65 to 55:45.

The polymerization can be carried out in a liquid phase process, or in agas phase process, or in a combination process of gas phase and liquidphase. In the case where the polymerization is carried out in liquidphase, polymerization temperature is in a range of from 0° C. to 150°C., and preferably from 40° C. to 100° C., and polymerization pressureis higher than saturated vapor pressure of propylene at thecorresponding polymerization temperature. In the case where thepolymerization is carried out in gas phase, polymerization temperatureis in a range of from 0° C. to 150° C., and preferably from 40° C. to100° C., and polymerization pressure may be normal pressure or higher,and preferably in a range of from 1.0 to 3.0 MPa (gauge, similarlyhereinafter).

Comonomers which may copolymerize with propylene in the processaccording to the invention include ethylene and C₄-C₁₂ α-olefins, forexample, 1-butene, 1-hexene, and 1-octene.

As mentioned above, the process of the invention may be performed ineither a continuous process or a batch process. In the case where acontinuous process is employed, the process of the invention may beperformed in two or more loop reactors in series, or in two or more tankreactors in series, or in two or more gas phase reactors in series, orin any combination of a loop reactor, a tank reactor, and a gas phasereactor. In the case where the first stage of polymerization is acontinuous liquid phase polymerization, it is preferable to subject thecatalyst to a continuous or batch prepolymerization. By subjecting thecatalyst to propylene prepolymerization, it is possible to controleffectively particle morphology of the polymers during the reaction, toreduce breaking of polymer particles, and for the catalyst to exerteffectively its catalytic activity. The prepolymerization is generallyconducted under mild conditions, wherein polymerization temperature ispreferably lower than 30° C., and prepolymerization rate is controlledas being in a range of from 3 to 1000 grams of PP per gram of thecatalyst. In the case where the first stage of polymerization is acontinuous gas phase polymerization, the catalyst may or may not besubjected to a prepolymerization.

In a particularly preferred embodiment, the process for preparingpolypropylenes having broad molecular weight distributions according tothe invention is one comprising successively performinghomopolymerization or copolymerization of propylene in two loop reactorsin series in the presence of a highly-stereoselective Ziegler-Nattacatalyst, which comprises a reaction product of an activetitanium-containing solid catalyst component, an organic aluminumcompound and an organic silicon compound, wherein in the first loopreactor, a weight ratio of the organic aluminum compound to the organicsilicon compound (also simply referred to as Al/Si weight ratio) is in arange of from 10 to 300, preferably from 30 to 150; an additional amountof the organic silicon compound is added in the second loop reactor sothat a Al/Si weight ratio in the second loop reactor is less than thatin the first loop reactor, preferably 2 to 20 times less than that inthe first loop reactor; a concentration of a molecular weight controlagent in the second loop reactor is larger than that in the first loopreactor; a ratio of the output of the first loop reactor to the outputof the second loop reactor is approximately in a range of from 35:65 to55:45; polymerization temperatures in the two loop reactors arecontrolled at 60 to 80° C.; and the polymerization is a liquid phasebulk polymerization.

Another aspect of the invention relates to polymers produced by theabove-described process of the invention. The polymers according to theinvention have broad molecular weight distribution, with polydispersityindex being in a range of from 3 to 10, and preferably from 4 to 8, andthe isotacticity of the low molecular weight fraction thereof is higherthan the isotacticity of the high molecular weight fraction thereof. Thepolymers according to the invention have excellent combined properties,in particular, remarkably improved mechanical properties. Additionally,since the low molecular weight fraction of the propylene polymers has arelatively high isotacticity, the problem that the low molecular weightfraction migrates out from the interior of materials during theprocessing of the resins or during the long-term use of articles isremoved.

The propylene polymers according to the invention may be furtherprocessed by processes well known in the art. For example, the polymersmay be pelletized through conventional equipment. During thepalletizing, additives commonly used in the art, such as antioxidants,light stabilizers, thermal stabilizers, colorants, and/or fillers can beadded into the polymers.

The pelletized or un-pelletized polymers of the invention can be used invarious possible applications of polypropylenes, such as biaxialoriented films, tubings, flat fibers, or injection mould articles.

Thus, another aspect of the invention relates to the articles preparedfrom the polypropylenes of the invention.

EXAMPLES

The invention will be described in detail with reference to specificexamples, which are illustrative but not restrictive.

The property data of the polymers given in the examples were obtained asfollows:

1. Isotactic index: measured according to a method described in GB2412-89.2. Pentad ([mmmm]) content by mole and average length of isotacticsequences (Nm): measured by Nuclear Magnetic Resonance SpectrometerModel AVANCE 400 from Bruker Co., Germany. A sample was dissolved indeuterated o-dichlorobenzene at 140° C., and measuring temperature was125° C. Experimental operation, assignment of peaks and date treatmentfollowed those as disclosed in literatures (see, for example, James C.Randall, Polymer Sequence Determination: ¹³Carbon NMR Method, Academic,New York, 1977).3. Melt flow rate (MFR): measured according to ISO1133-05, 230° C., 2.16kg loading.4. Polydispersity index: viscosities and moduli of a sample weremeasured on ARES rheometer from Rheometric Scientific Inc., USA equippedwith a plate clamp at 190° C. over a certain frequency range.Polydispersity index (PI) was calculated as PI=10⁵/G, in which G is amodulus value at the crossing of the storage modulus (G′) versefrequency curve and the loss modulus (G″) verse frequency curve. Priorto the measurement, the resin sample was compression mould at 200° C.into a plate of 2 mm thickness (see L. A. Utracki and A. Luciani,Rheology of polypropylene in Karger-Kocsis J., ed., Polypropylene: A-ZReference, Dordrecht: Kluwer Publishers, 1999, 716).5. Tensile strength of resin: measured according to ASTM D638-00.6. Flexural modulus of resin: measured according to ASTM D790-97.7. Izod impact strength: measured according to ASTM D256-00.

Example 1

A main catalyst (active titanium-containing solid catalyst component)was prepared by the process described in Example 1 of Chinese patentapplication CN93102795. The main catalyst was found to have a Ti contentof 2.4 wt %, a Mg content of 18.0 wt %, and a di-n-butyl phthalatecontent of 13 wt %.

Polymerization was performed in a polypropylene pilot plant using two 75L loop polymerization reactors. The main catalyst, cocatalyst (i.e.,triethylaluminum), and external electron donor (i.e., cyclohexyl methyldimethoxy silane) pre-contacted with each other at 10° C. for oneminute, and then were continuously fed into a 2 L prepolymerizationreactor to conduct prepolymerization. Flow rate of each raw material fedinto the prepolymerization reactor was 5.29 g/hr for triethyl aluminum,0.13 g/hr for cyclohexyl methyl dimethoxy silane, 0.01 g/hr for the maincatalyst, and 11 kg/hr for propylene. Prepolymerization temperature was15° C., prepolymerization pressure was 4.1 MPa, and residence time was 6minutes.

The stream from the prepolymerization reactor was continuously fed intothe first reactor of the two loop reactors in series, to catalyzehomopolymerization of propylene. Al/Si weight ratio in the first loopreactor was 40. Polymerization temperature in the two loop reactors was70° C., pressure in the two loop reactors was 4.1 MPa, and residencetime was 1.1 hours for the first loop reactor and 0.8 hours for thesecond loop reactor. Propylene was fed into the first loop reactor at aflow rate of 23 kg/hr and into the second loop reactor at a flow rate of12 kg/hr. The feed to the first loop reactor contained hydrogen gas at aconcentration of 180 ppm by volume, and additional hydrogen gas wasadded into the feed to the second loop reactor so that hydrogen gasconcentration reached 2600 ppm by volume. Additional cyclohexyl methyldimethoxy silane was fed into the second loop reactor at a flow rate of0.4 g/hr, so that Al/Si weight ratio in the second loop reactor was 10.The ratio of the output of the first loop reactor to the output of thesecond loop reactor was 45:55.

To the powdery polymer resulted from the polymerization were added 0.1wt % of IRGAFOS 168, 0.2 wt % of IRGANOX 1010 and 0.05 wt % of calciumstearate, and the resulting mixture was pelletized through a twin screwextruder. Properties of the resultant pellets were measured and theresults are shown in the Table 1 below.

Example 2

The procedure as described in the Example 1 was followed, except thatthe flow rate of cyclohexyl methyl dimethoxy silane fed to theprepolymerization reactor was changed to 0.06 g/hr so that Al/Si weightratio in the first loop reactor was 80, and additional cyclohexyl methyldimethoxy silane was fed into the second loop reactor at a flow rate of0.47 g/hr, so that Al/Si weight ratio in the second loop reactor was 10.The results of property measurement are shown in the Table 1.

Example 3

The procedure as described in the Example 1 was followed, except thatthe hydrogen concentration in the feed to the first loop reactor wascontrolled at 80 ppm by volume, and the hydrogen concentration in thefeed to the second loop reactor was controlled at 5200 ppm by volume.The results of property measurement are shown in the Table 1.

Comparative Example 1

The procedure as described in the Example 1 was followed, except thatcyclohexyl methyl dimethoxy silane as external electron donor was fedinto only the prepolymerization reactor at a flow rate of 0.13 g/hr (inorder words, no cyclohexyl methyl dimethoxy silane was added into thesecond loop reactor), so that Al/Si weight ratio in both the two loopreactors was 40.

Comparative Example 2

The procedure as described in the Example 1 was followed, except thatcyclohexyl methyl dimethoxy silane as external electron donor was fedinto only the prepolymerization reactor at a flow rate of 0.53 g/hr (inorder words, no cyclohexyl methyl dimethoxy silane was added into thesecond loop reactor), so that Al/Si weight ratio in both the two loopreactors was 10.

It can be seen from the data obtained in the Examples and theComparative Examples that polymers having better combined properties, inparticular, remarkably improved mechanical properties can be obtained byadjusting stereoselectivities of active sites of the catalyst underdifferent hydrogen concentrations, namely, increasing the amount of theexternal electron donor component used in the second polymerizationstage for producing low molecular weight fraction of the polymers so asto make a ratio of the isotacticity of the final polymer to theisotacticity of the propylene polymer produced in the firstpolymerization stage larger than 1.

TABLE 1 Process conditions for Examples 1-4 and Comparative Examples 1-2and properties of resins Comparative Comparative Example 1 Example 2Example 3 Example 1 Example 2 1#Loop 2#Loop 1#Loop 2#Loop 1#Loop 2#Loop1#Loop 2#Loop 1#Loop 2#Loop Reactor Reactor Reactor Reactor ReactorReactor Reactor Reactor Reactor Reactor Process Conditions H₂concentration ppmv 180 2600 180 2600 80 5200 180 2600 180 2600 in thefeed Al/Si weight ratio* wt/wt 40 10 80 10 40 10 40 40 10 10 Product**MFR g/10 min 0.75 2.8 0.82 2.9 0.36 2.6 0.73 3.1 0.84 2.7 Isotacticitywt % 96.3 96.7 94.5 95.2 96.8 96.9 96.6 96.5 98.8 97.6 Nm measured by31.1 36.8 27.9 33.5 31.6 39.4 32.5 32.0 53.6 53.2 ¹³C-NMR [mmmm] contentmol % 82.3 84.7 81.2 83.6 83.1 85.1 83.3 83.2 88.7 88.7 measured by¹³C-NMR Polydispersity index 5.7 5.8 6.8 5.8 5.7 (PI) Tensile strengthMPa 35.4 35.1 Flexural strength MPa 38.2 29.5 Flexural modulus GPa 1.391.11 IZOD notched impact J/m 52 53 strength *Weight ratio of triethylaluminum to cyclohexyl methyl dimethoxy silane **The product of 1# LoopReactor or 2# Loop Reactor means a sample taken from correspondingreactor.

The patents, patent applications, non-patent literatures and testingmethods cited in the specification are incorporated herein by reference.

While the invention has been described with reference to exemplaryembodiments, it will be understood by those skilled in the art thatvarious changes and modifications may be made without departing from thespirit and scope of the invention. Therefore, the invention is notlimited to the particular embodiments disclosed as the best modecontemplated for carrying out this invention, but the invention willinclude all embodiments falling within the scope of the appended claims.

1. A process for preparing a polypropylene having broad molecular weightdistribution, the process comprising at least the following two stagesof polymerization: a first stage of polymerization, which ishomopolymerization of propylene or copolymerization of propylene and anα-olefin carried out in the presence of a Ziegler-Natta catalyst and aless amount of a molecular weight control agent, to provide a highmolecular weight fraction of the polypropylene; and a second stage ofpolymerization, which is homopolymerization of propylene orcopolymerization of propylene and an α-olefin carried out in thepresence of the resulting polymer from the first stage of polymerizationand a larger amount of the molecular weight control agent, to provide alow molecular weight fraction of the polypropylene, wherein the firststage of polymerization employs optionally an external electron donorcompound, and the second stage of polymerization employs an externalelectron donor compound, wherein the amount and/or kind of the externalelectron donor compound used in the second stage of polymerizationare/is selected so as to give a final polymer having an isotacticityhigher than that of the polymer produced in the first stage ofpolymerization, and wherein a ratio of the output of the first stage ofpolymerization to the output of the second stage of polymerization is ina range of from 30:70 to 70:30.
 2. The process according to claim 1,wherein a ratio of the MFR value of the final polymer to the MFR valueof the propylene polymer prepared in the first stage of polymerizationis in a range of from 5 to
 15. 3. The process according to claim 1,wherein a ratio of the isotacticity of the final polymer to theisotacticity of the propylene polymer prepared in the first stage ofpolymerization is larger than 1 but less than or equal to 1.2.
 4. Theprocess according to claim 1, wherein the Ziegler-Natta catalyst used inthe first stage of polymerization is a reaction product of: a solidcatalyst component comprising magnesium, titanium, a halogen and aninternal electron donor as essential components, an organic aluminumcompound, and an organic silicon compound, with a weight ratio of theorganic aluminum compound to the organic silicon compound being in arange of from 10 to 300, and wherein an additional amount of the organicsilicon compound is added in the second stage of polymerization so as togive a weight ratio of the organic aluminum compound to the organicsilicon compound less than that in the first stage of polymerization. 5.The process according to claim 4, wherein the weight ratio of theorganic aluminum compound to the organic silicon compound in the firststage of polymerization is 2 to 20 times larger than that in the secondstage of polymerization.
 6. The process according to claim 1, whereinthe process comprises the first and second stages of polymerization, andthe first and second stages of polymerization are carried out in a firstloop reactor and a second loop reactor in series, respectively.
 7. Theprocess according to claim 6, wherein the ratio of the output of thefirst stage of polymerization to the output of the second stage ofpolymerization is in a range of from about 35:65 to about 55:45,polymerization temperatures in the two loop reactors are controlled at60 to 80° C., and the polymerization is conducted in a liquid phase bulkprocess.
 8. A process for preparing a polypropylene having broadmolecular weight distribution, the process comprising successivelyperforming homopolymerization or copolymerization of propylene in twoloop reactors in series in the presence of a highly-stereoselectiveZiegler-Natta catalyst, which comprise a reaction product of an activetitanium-containing solid catalyst component, an organic aluminumcompound and an organic silicon compound, wherein in the first loopreactor, a weight ratio of the organic aluminum compound to the organicsilicon compound is in a range of from 10 to 300; an additional amountof the organic silicon compound is added in the second loop reactor sothat a weight ratio of the organic aluminum compound to the organicsilicon compound in the second loop reactor is less than that in thefirst loop reactor; a concentration of a molecular weight control agentin the second loop reactor is larger than that in the first loopreactor; a ratio of the output of the first loop reactor to the outputof the second loop reactor is in a range of from about 35:65 to about55:45; polymerization temperatures in the two loop reactors arecontrolled at 60 to 80° C.; and the polymerization is a liquid phasebulk polymerization.
 9. The process according to claim 8, wherein theweight ratio of the organic aluminum compound to the organic siliconcompound in the first loop reactor is 2 to 20 times larger than that inthe second loop reactor.
 10. A polypropylene preparable by the processas claimed in claim
 1. 11. A polypropylene preparable by the process asclaimed in claim
 8. 12. A polypropylene, which has a polydispersityindex of 3 to 10, and of which the isotacticity of the low molecularweight fraction is higher than the isotacticity of the high molecularweight fraction.
 13. Biaxial oriented films, tubings, flat fibers, orinjection mould articles prepared from the polypropylene as claimed inclaim
 10. 14. Biaxial oriented films, tubings, flat fibers, or injectionmould articles prepared from the polypropylene as claimed in claim 11.15. Biaxial oriented films, tubings, flat fibers, or injection mouldarticles prepared from the polypropylene as claimed in claim 12.